EP0777638B1 - Procede de production de pentafluoroethane - Google Patents

Procede de production de pentafluoroethane Download PDF

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Publication number
EP0777638B1
EP0777638B1 EP95927866A EP95927866A EP0777638B1 EP 0777638 B1 EP0777638 B1 EP 0777638B1 EP 95927866 A EP95927866 A EP 95927866A EP 95927866 A EP95927866 A EP 95927866A EP 0777638 B1 EP0777638 B1 EP 0777638B1
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EP
European Patent Office
Prior art keywords
hcfc
fluorination
pentafluoroethane
reactor
hfc
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
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EP95927866A
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German (de)
English (en)
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EP0777638A1 (fr
Inventor
Charles John Shields
Paul Nicholas Ewing
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Ineos Fluor Holdings Ltd
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Imperial Chemical Industries Ltd
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
    • C07C17/20—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms
    • C07C17/21—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms with simultaneous increase of the number of halogen atoms

Definitions

  • This invention relates to a process for the manufacture of pentafluoroethane [HFC 125] and particularly to a process comprising the manufacture of pentafluoroethane by reacting perchloroethylene with hydrogen fluoride in the gas phase over a fluorination catalyst such as chromia
  • HCFC 123 and HCFC 124 are readily separated from the product stream by distillation and can be recycled to the hydrofluorination reactor for further fluorination
  • HCFC 133a and HFC 134a are also readily separated from the pentafluoroethane product stream by distillation but these cannot be fluorinated to pentafluoroethane by recycling them to the hydrofluorination reactor so they are generally removed from the process.
  • the impurities in the organic product stream which may be present in an appreciable amount, for example up to 10 - 20% by weight, range from low boiling compounds (or lights) to high boiling compounds (or heavies) relative to pentafluoroethane and their removal from the stream usually is effected sequentially in a series of distillation columns.
  • the stream from the fluorination reactor may be fed to a first column from which hydrogen fluoride, dichlorotrifluoroethane [HCFC 123/123a] and other heavies are removed as a bottom fraction whilst the remainder of the stream is removed as a top fraction.
  • the bottom faction from this first column may be recycled to the fluorination reactor.
  • the top fraction from the first column may be fed to a second distillation column from which pentafluoroethane [HFC 125] is withdrawn together with chloropentafluoroethane [CFC 115] as a top faction whilst the remainder of the stream, comprising mainly chlorotetrafluoroethane [HCFC 124/124a], chlorotrifluoroethane [HCFC 133/133a], tetrafluoroethane [HFC 134/134a] and dichlorotetrafluoroethane [CFC 114/144a] is withdrawn as a bottom fraction.
  • the pentafluoroethane (containing chloropentafluoethane) withdrawn as a top fraction may be further treated to effect purification of the pentafluoroethane.
  • the bottom fraction from the second column may be fed to a third distillation column from which tetrafluoroethane [HFC 134/134a] is withdrawn as a top fraction and removed from the system whilst the remainder of the stream is withdrawn as a bottom fraction and passed to a fourth distillation column from which chlorotetrafluoroethane [HCFC 124/124a] is withdrawn as a top fraction whilst dichlorotetrafluoroethane [CFC 114/114a] and chlorotrifluoroethane [HCFC 133/133a] are withdrawn as a bottom fraction.
  • HFC 134/134a tetrafluoroethane
  • the chlorotetrafluoroethane [HCFC 124/124a] may be recycled to the fluorination reactor for fluorination to pentafluoroethane [HFC 125].
  • the amounts of CFC 114/114a and HCFC 133/133a in the bottom fraction from the fourth column is usually so low that recovery of the components is not economic and the mixture is usually disposed of, for instance by thermal oxidation.
  • aqueous scrubbing is optional. Where this step is excluded, the various top and bottom fractions from the columns may contain hydrogen fluoride in addition to the components recited and the various components may be in the form of azeotropes or azeotrope-like compositions with hydrogen fluoride.
  • a process for the manufacture of pentafluoroethane by reaction of perchloroethylene with hydrogen fluoride in the vapour phase over a fluorination catalyst in a fluorination reactor with recycle of dichlorotrifluoroethane and chlorotetrafluoroethane to the fluorination reactor wherein tetrafluoroethane is also recycled to the fluorination reactor.
  • the recycled tetrafluoroethane [HFC 134/134a] reacts with hydrogen chloride produced in the reactor to form chlorotrifluoroethane [HCFC 133a].
  • HCFC 133a is subsequently removed from the process (and usually is disposed of by thermal oxidation).
  • recycling tetrafluoroethane [HFC 134/134a] to the fluorination reactor results in removal of tetrafluoroethane from the process.
  • Figs 1 and 2 show flow sheets of processes in which tetrafluoroethane [HFC 134a] is separated together with chlorotetrafluoroethane [HCFC 124] and recycled to a fluorination reactor in which pentafluoroethane is produced by reaction of perchloroethylene with hydrogen fluoride.
  • the difference between the processes is that in Fig 1 the intermediate dichlorotetrafluoroethane [HCFC 123] is separated in a single distillation column whilst in fig 2 the HCFC 123 is separated in two distillation columns.
  • perchloroethylene and hydrogen fluoride are fed as stream 1 to a fluorination reactor 2 containing a fluorination catalyst (for example chromia or zinc-promoted chromia) and heated at 200 - 400°C.
  • a fluorination catalyst for example chromia or zinc-promoted chromia
  • the resulting product stream comprising pentafluoroethane and intermediates and impurities is fed via 3 to a first distillation column 4 operating at a pressure of 8- 12 bar and temperature of 20 - 40°C.
  • HCFC 123, hydrogen fluoride and other relatively high boiling compounds (heavies) are withdrawn from the bottom of column 4 via 5 and recycled to the fluorination reactor 2 together with the perchloroethylene and hydrogen fluoride fed via 1.
  • the remaining product stream withdrawn from the top of column 4 via 6 is scrubbed with water, dried and compressed at 7 and fed via 8 to a second distillation column 9 operating at a pressure of 2.5-20 bar and a temperature of -25 to +45°C.
  • Pentafluoroethane [HFC 125] is withdrawn from the top of column 9 via 10 together with chloropentafluoroethane [CFC 115] and the remaining product stream is withdrawn from the bottom of the column via 11 and fed to a third distillation column 12.
  • HFC 134a tetrafluoroethane
  • HCFC 124 chlorotetrafluoroethane
  • Dichlorotetrafluoroethanes [CFC 114/114a] and chlorotrifluoroethane [HCFC 133a] are withdrawn from the bottom of column 12 and fed via 14 to e.g. a thermal oxidiser for disposal.
  • the process shown in Fig 2 is similar to that shown in Fig 1 except that the first distillation column 4 is operated to separate part only of the dichlorotrifluoroethane [HCFC 123].
  • the process includes a fourth distillation column 15 from which dichlorotrifluoroethane [HCFC 123] is withdrawn as a bottom fraction via 16 and is recycled to the fluorination reactor 2 whilst dichlorotetrafluoroethanes [CFC 114/114a] and chlorotrifluoroethane [HCFC 133a] are withdrawn as a top faction and fed via 17 to e.g. a thermal oxidiser.
  • tetrafluoroethane [HFC 134a] is converted to chlorotrifluoroethane [HFC 133a] in the fluorination reactor and the HCFC 133a is subsequently removed from the system so that HFC 134a is removed from the pentafluoroethane product stream without the need to provide a dedicated distillation column to effect the separation.
  • the overall effect of the process according to the invention is the removal of the 13 * series products (HFC 134a and HCFC 133a) from the pentafluoroethane product stream, the technique relying on the conversion of HFC 134a to HCFC 133a by reaction with by-product hydrogen chloride in the fluorination reactor.
  • a competing reaction in the fluorination reactor is the reaction of HCFC 133a with hydrogen fluoride to produce HFC 134a so that an alternative technique for removing the 13* series products from the pentafluoroethane product stream would be to remove the HFC 134a from the system and recycle the HCFC 133a.
  • this alternative technique suffers from the disadvantage that a large volume of HCFC 133a has to be recycled.
  • the fluorination of HCFC 133a to produce HFC 134a is equilibrium - limited and under typical operating conditions to make HFC 125, the conversion of HCFC 133a to HFC 134a is only about 5% per pass through the fluonnation reactor and a large volume of HCFC 133a has to be recycled.
  • this alternative technique for removing the 13* series products would involve a recycle stream in which HCFC 133a is one ofthe major components and accounts for up to a third or more of the recycle stream.
  • the technique according to the invention involves the recycle of an extremely small volume of HFC 134a. Minimising the volume of the recycle stream is a further advantage provided by the process according to the invention.
  • the above description of the invention with reference to the drawings includes a guide as to the operating conditions for the fluorination reactor and distillation columns used to produce and treat the pentafluoroethane product stream but it is to be understood that this is by way of a guide only.
  • the operating conditions are well known in the art.
  • the catalyst in the fluonnation reactor typically will be and preferably is a chromia-based catalyst.
  • the tetrafluoroethane is removed from the product stream and recycled together with the HCFC 124. It is a simple matter to determine the optimum operating conditions for a distillation column to effect the removal of both HFC 134a and HCFC 124, optionally together with hydrogen fluoride. As a guide typical operating conditions are a superatmospheric pressure of from 2 to 8 bars and a temperature of 0°C to 50°C but it will be appreciated that operation under these conditions is not an essential feature of the invention.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de production de pentafluoroéthane [HFC 125] par réaction du perchloroéthylène avec du fluorure d'hydrogène en phase vapeur, en présence d'un catalyseur de fluoration, dans un réacteur de fluoration, avec recyclage du dichlorotrifluoroéthane [HCFC 123], du chlorotétrafluoroéthane [HCFC 124] et également du tétrafluoroéthane [HFC 134a] vers le réacteur de fluoration. Le tétrafluoroéthane et le chlorotétrafluoroéthane peuvent être, l'un et l'autre, séparés du flux de produits dans une seule colonne de distillation puis recyclés ensemble vers le réacteur de fluoration.

Claims (6)

  1. Procédé de production de pentafluoroéthane par réaction de perchloroéthylène avec du fluorure d'hydrogène en phase vapeur sur un catalyseur de fluoration dans un réacteur de fluoration en recyclant le dichlorotrifluoroéthane et le chlorotétrafluoroéthane au réacteur de fluoration, caractérisé en ce que le tétrafluoroéthane est également recyclé au réacteur de fluoration, dans lequel il est converti en chlorotrifluoroéthane qui est ensuite éliminé du réacteur par réaction avec le chlorure d'hydrogène produit dans le réacteur.
  2. Procédé selon la revendication 1, dans lequel le tétrafluoroéthane est séparé du courant de pentafluoroéthane produit et recyclé conjointement avec le chlorotétrafluoroéthane.
  3. Procédé selon la revendication 2, dans lequel la séparation du tétrafluoroéthane et du chlorotétrafluoroéthane du courant de produit est réalisée dans une seule colonne de distillation.
  4. Procédé selon la revendication 3, dans lequel la colonne de distillation opère à une pression de 1,6 à 20 bars.
  5. Procédé selon la revendication 2 ou 3, dans lequel la colonne de distillation opère à une température de 0°C à 70°C.
  6. Procédé selon l'une quelconque des revendications précédentes, dans lequel le catalyseur de fluoration est un catalyseur à base d'oxyde de chrome.
EP95927866A 1994-08-24 1995-08-08 Procede de production de pentafluoroethane Expired - Lifetime EP0777638B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
GB9417116 1994-08-24
GB9417116A GB9417116D0 (en) 1994-08-24 1994-08-24 Process for the manufacture of pentafluoroethane
PCT/GB1995/001872 WO1996006062A1 (fr) 1994-08-24 1995-08-08 Procede de production de pentafluoroethane

Publications (2)

Publication Number Publication Date
EP0777638A1 EP0777638A1 (fr) 1997-06-11
EP0777638B1 true EP0777638B1 (fr) 2000-01-05

Family

ID=10760344

Family Applications (1)

Application Number Title Priority Date Filing Date
EP95927866A Expired - Lifetime EP0777638B1 (fr) 1994-08-24 1995-08-08 Procede de production de pentafluoroethane

Country Status (13)

Country Link
US (1) US5962753A (fr)
EP (1) EP0777638B1 (fr)
JP (1) JP3843125B2 (fr)
CN (1) CN1057516C (fr)
CA (1) CA2197060A1 (fr)
DE (1) DE69514369T2 (fr)
ES (1) ES2141370T3 (fr)
GB (1) GB9417116D0 (fr)
HK (1) HK1002656A1 (fr)
MX (1) MX9701172A (fr)
PT (1) PT777638E (fr)
WO (1) WO1996006062A1 (fr)
ZA (1) ZA956775B (fr)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3496708B2 (ja) 1997-10-09 2004-02-16 ダイキン工業株式会社 １，１，１，２，２−ペンタフルオロエタンの製造方法
FR2894250B1 (fr) * 2005-12-06 2008-01-18 Arkema Sa Procede de fabrication du pentafluoroethane
FR2901790A1 (fr) * 2006-05-30 2007-12-07 Arkema France Procede de fabrication des hydrofluorocarbures
FR2901789B1 (fr) * 2006-05-30 2009-04-24 Arkema France Procede de fabrication des hydrofluorocarbures
FR2901788B1 (fr) * 2006-05-30 2008-07-18 Arkema France Procede de fabrication du pentafluoroethane
FR2907449B1 (fr) * 2006-10-20 2009-01-02 Arkema France Procede de fabrication du pentafluorethane.
JP5146466B2 (ja) * 2007-12-14 2013-02-20 ダイキン工業株式会社 ペンタフルオロエタンの製造方法

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB901297A (en) * 1960-04-12 1962-07-18 Union Carbide Corp Process for the production of pentafluoroethane
GB9104775D0 (en) * 1991-03-07 1991-04-17 Ici Plc Fluorination catalyst and process
GB9325756D0 (en) * 1993-12-16 1994-02-16 Ici Plc Production of pentafluoroethane

Also Published As

Publication number Publication date
US5962753A (en) 1999-10-05
ES2141370T3 (es) 2000-03-16
ZA956775B (en) 1996-02-26
HK1002656A1 (en) 1998-09-11
WO1996006062A1 (fr) 1996-02-29
CN1057516C (zh) 2000-10-18
MX9701172A (es) 1997-05-31
JP3843125B2 (ja) 2006-11-08
JPH10505341A (ja) 1998-05-26
DE69514369D1 (de) 2000-02-10
CA2197060A1 (fr) 1996-02-29
PT777638E (pt) 2000-04-28
CN1160390A (zh) 1997-09-24
GB9417116D0 (en) 1994-10-12
DE69514369T2 (de) 2000-10-19
EP0777638A1 (fr) 1997-06-11

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